WO1979000589A1 - Procede et installation pour la recuperation du fluide de travail d'un echangeur de chaleur a contact direct - Google Patents

Procede et installation pour la recuperation du fluide de travail d'un echangeur de chaleur a contact direct Download PDF

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Publication number
WO1979000589A1
WO1979000589A1 PCT/US1979/000052 US7900052W WO7900589A1 WO 1979000589 A1 WO1979000589 A1 WO 1979000589A1 US 7900052 W US7900052 W US 7900052W WO 7900589 A1 WO7900589 A1 WO 7900589A1
Authority
WO
WIPO (PCT)
Prior art keywords
working fluid
water containing
steam
brine
column
Prior art date
Application number
PCT/US1979/000052
Other languages
English (en)
Inventor
E Wahl
Original Assignee
Occidental Petroleum Corp
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Occidental Petroleum Corp filed Critical Occidental Petroleum Corp
Publication of WO1979000589A1 publication Critical patent/WO1979000589A1/fr

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F03—MACHINES OR ENGINES FOR LIQUIDS; WIND, SPRING, OR WEIGHT MOTORS; PRODUCING MECHANICAL POWER OR A REACTIVE PROPULSIVE THRUST, NOT OTHERWISE PROVIDED FOR
    • F03G—SPRING, WEIGHT, INERTIA OR LIKE MOTORS; MECHANICAL-POWER PRODUCING DEVICES OR MECHANISMS, NOT OTHERWISE PROVIDED FOR OR USING ENERGY SOURCES NOT OTHERWISE PROVIDED FOR
    • F03G7/00—Mechanical-power-producing mechanisms, not otherwise provided for or using energy sources not otherwise provided for
    • F03G7/04—Mechanical-power-producing mechanisms, not otherwise provided for or using energy sources not otherwise provided for using pressure differences or thermal differences occurring in nature
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E10/00—Energy generation through renewable energy sources
    • Y02E10/10—Geothermal energy
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S203/00—Distillation: processes, separatory
    • Y10S203/21—Acrylic acid or ester

Definitions

  • This invention relates to the recovery of working fluid entrained in the spent geothermal brine or other hot water source withdrawn from a direct contact heat exchanger in which heat is transferred from the brine or hot water to the working fluid, and is particularly concerned with a process and system of the aforementioned type, including removal of the working fluid contained in the spent geothermal brine or hot water source, by a series of successive steps or operations, whereby the final spent brine or water removed from the system is substantially free or has a very small concentration of remaining working fluid, and wherein the working fluid so recovered is recycled to the direct contact heat exchange column.
  • Patent 3,988,895 discloses the step of removing entrained working fluid from the spent brine in a separator, followed by flashing off additional working fluid from the spent brine.
  • one object of the present invention is the efficient removal and recovery of working fluid entrained and/or dissolved in the spent geothermal brine or hot water withdrawn from a direct contact heat exchanger used for recovery of energy from such geothermal brine or hot water.
  • Another object is the provision of an economical process and system of the above type, including subjecting the spent brine or hot water from the direct contact heat exchanger to a series of successive operations or steps, for removal of substantially all of the entrained working fluid from the spent brine or hot water and for recycling of such recovered working fluid to the direct contact heat exchanger.
  • a still further object of the invention is the carrying out of such operations or steps for recovery of working fluid contained in the spent brine or hot water, with a minimum energy expenditure.
  • the geothermal brine from a well or other hot water containing source is introduced under pressure into a heat exchanger in direct heat exchange contact with an immiscible working fluid such as isobutane.
  • an immiscible working fluid such as isobutane.
  • the resulting hot working fluid is expanded in an expander or turbine to produce work, and the expanded working fluid discharged .from the turbine is condensed and the condensed working fluid is returned to the heat exchanger.
  • the cooled brine containing some entrained and/or dissolved working fluid is withdrawn from the heat exchange column.
  • the spent brine or water is first passed to a settling tank to separate and recover some of the immiscible working fluid, the resulting spent brine or water is then flashed in a flash drum, to further reduce the working fluid content of the spent brine or water, and the spent brine or water is then subjected to steam stripping for still
  • K 1P further reducing the working fluid content of the spent brine or water.
  • the steam stripping stage or step results in removing substantially all or the major portion of the remaining working fluid content from the spent brine or water.
  • the recovered working fluid in each of the above three stages or operations is collected and recycled to the direct contact heat exchanger. If the spent brine or hot water leaving the direct contact heat exchange column is at sufficiently high pressure, energy can be recovered between the above noted first and second stages of working fluid recovery, by a work expander or power recovery turbine.
  • the second stage which comprises flashing the resulting spent brine or water, involves dropping the pressure of the solution to the pressure of the condenser used in condensing the working fluid dis ⁇ charged from the turbine in the basic process, so that the working fluid, e.g. isobutane, will boil from the solution and flow overhead to the condenser for recovery therein, followed by passage of the condensed working fluid back to the direct contact heat exchanger.
  • the working fluid e.g. isobutane
  • the resulting spent brine or hot water is subjected to steam stripping for further working fluid recovery.
  • the spent brine or water containing the working fluid enters the top of the stripping column while steam flowing upwardly in the column carries working fluid out of the top of the column.
  • the steam for such stripping can be generated by using the heat of the spent brine or hot water, and if desired, by additional use of some hot wellhead brine, external steam or other heat source for this purpose.
  • the mixture of working fluid and steam which is carried from the*top of the stripper is condensed, the gaseous working fluid is separated from the condensed steam and is returned to the condenser for the working fluid discharged from the turbine in the basic process, for recycling to the direct contact heat exchanger.
  • FIG. 1 is a schematic flow diagram of the basic direct contact heat exchange power generation system employing direct contact heat exchanger; and FIG. 2 is a schematic flow sheet of one preferred embodiment of the invention for recovery of working fluid from spent geothermal brine removed from the direct contact heat exchanger of Fig. 1.
  • geothermal brine or hot water which may be degassed to partially remove non-condensible gases, enters through inlet means or conduit 10 and is passed to pump 12 which discharges via valve 14 and conduit 16 into an inlet 18 ⁇ from which the hot water or brine is discharged into the top of the heat exchanger column 20 in direct contact heat exchange with a working fluid.
  • Such working fluid can be any suitable material which is immiscible with water, and such working fluid can have a density less than or greater than the density of the hot water con ⁇ taining fluid or brine, provided that the same density relation exists along the length of the column, so as to provide countercurrent flow of working fluid and water-containing fluid such as brine in the column.
  • the working fluid can be a hydrocarbon including aromatics, paraffins, naphthenes and olefins.
  • the working fluid is a paraffin or olefinic
  • paraffinic or olefinic hydro ⁇ carbons containing from about 3 to about 6 carbon atoms are employed.
  • Aromatic hydrocarbons such as benzene, toluene, and xylene also can be used.
  • Mixtures of such hydrocarbons can also be utilized, such as, for example, a mixture of methane and ethane, ethane and propane, or propane and n-butane, to optimize the critical temperature and pressure conditions of the working fluid, and thereby obtain maximum energy recovery from the geothermal brine or hot water feed.
  • Working fluids other than hydrocarbons are also suitable provided they at least have the proper density relation to the hot aqueous fluid or brine as _ noted above and are immiscible.
  • a particularly preferred working fluid is isobutane.
  • Inlet temperature of the hot water or brine to the top of the column ranges from about 150°F.
  • the heat exchange column 20 can be operated above, or below, or at the critical conditions of the working fluid, in one embodiment the heat transfer column is operated above the critical pressure of the working fluid in the top of the column,
  • wip such pressure preferably ranging, in absolute terms
  • the working fluid is heated in heat exchange column 20 by direct contact with the incoming hot brine or hot water.
  • an inlet nozzle 22 can be provided at the top of the column, for directing the hot brine or hot water downwardly into the column.
  • the discharged expander working fluid is then passed via conduit 32 to a cooler or condenser 34, and the condensed working fluid is then removed through line 36 and pump 38 to pressurize the working fluid approximately to the pressure in the heat exchanger column 20 and the pres- surized fluid is then fed via valve 40 and conduit 42 to the inlet 44, through which the cold working fluid is introduced into the bottom of the heat exchanger column 20, to be reheated therein. Cooled brine or water in the bottom of the heat exchange column is discharged at 46.
  • the heat transfer column 20 can be of any conventional type such as one containing dual flow trays or sieve plates, as indicated schematically at 48, to provide efficient heat transfer between the
  • Such first stage of the working fluid recovery process and system of the invention comprises settling of the brine or water in a settling tank 52 for recovery of a portion of the working fluid in liquid form.
  • a throttling valve 54 it is preferred to lower the pressure of the working fluid by passage of the working fluid first through a throttling valve 54 prior to introduction into the settling tank 52, to lower the solubility of the working fluid in the brine or water, and permit greater recovery of the working fluid in liquid form.
  • a work expander or turbine can be employed to reduce the pressure of the brine or water, and at the same, time recover .useful energy.
  • the liquid working fluid withdrawn from the settling tank 52 at 56 is pumped at 58 up to the pressure in the heat transfer column 20 and is returned via line 60 and conduit 42 (Fig. 1) to the heat transfer column 20.
  • the brine or water in the settling tank 52 is discharged at 62 and fed to a turbine 64 for recovery of power, while dropping the pressure of the discharged brine or water at 66 to the pressure in the condenser or cooler 34 (see Fig. 1) .
  • the brine or water in line 66 is introduced into the second stage B of the working fluid recovery process and system of the invention, which comprises a flash drum 68. Additional working fluid, e.g. isobutane,
  • O P ⁇ entrained and/or dissolved in the brine or water is boiled from the solution in flash drum 68 and flows overhead via conduit 70 and is introduced into the condenser 34 (see Fig. 1) .
  • the only energy required in this stage is for boiling the working fluid, and such energy is provided by -the hot solution itself.
  • the brine or water discharged from the flash drum 68 is passed via line 72 to the third stage C of the invention working fluid recovery system and process.
  • Such third stage comprises a stripping column 74 of . conventional type, containing a plate system as indi ⁇ cated at 76, the brine or water at 72 being introduced through a coil 78 in the lower portion of the stripper 74 in indirect heat exchange with the lower portion of the stripper, and then passed via conduit 80 to an inlet 82 in the top of column 74.
  • the brine or water containing the working fluid thus enters the top of the column and flows down across the plates 76 or equivalent contacting devices.
  • the steam fox. the stripping operation. can be_ generated by the brine or- water passing through coil 78.
  • wellhead brine or steam or other heat source can be introduced at 84 into the stripper 74 to provide the heat drive for operating the stripper.
  • Such mix ⁇ ture is then conducted to a cooler or condenser 88, from which the condensed liquid is passed to a settler 90.
  • the condensed steam or water is discharged at 92, and the working fluid in gaseous form discharged from the settler 9Q, is conducted via line 94 to a pump 96, to pump the working fluid up to the pressure in condenser 34 (see Fig. 1) , and the resulting working fluid is conducted via conduit 98 into conduit 70 (see Fig. 1) for introduction into the condenser 34.
  • the waste brine or water is discharged at 100 from the third stage stripper 74, and is discarded by passage to a sump or to a brine injection well (not shown).
  • the brine or water.thus discharged at 100 has a very low working fluid content, and can be considered to be substantially free of any recoverable amount of working fluid.
  • spent brine containing isobutane working fluid withdrawn at 46 from the direct contact heat transfer column 20, and at a temperature of 190°F. (87.8°C.) and at a pressure
  • the brine withdrawn from the settling tank is introduced as feed into a power recovery turbine, and the discharged brine from the turbine at a reduced
  • the resulting brine is then introduced first through the bottom of a stripper in indirect heat exchange contact with the lower portion of the stripper, and is then introduced into the top of the stripper.
  • Wellhead brine at 340°F. (171.1°C.) is introduced direct ⁇ ly into the lower portion of the stripper.
  • a mixture of steam and isobutane at about 130°F. (54.4°C.) is recovered as overhead from the stripper and is condensed, the noncondensed isobutane gas being pumped up to the
  • the brine discharged from the stripper is mixed with the condensed steam in the overhead from the stripper, and is discarded.
  • the isobutane content of the brine dis ⁇ charged from the stripper is 1 ppm or less, which is not practically recoverable, and thus such spent brine is considered to be substantially free of working .fluid.
  • the brine in the stripping column of the third stage of the recovery process and system is cooled from 150°F. (65.56°C.) to 130°F. (54.4°C) , and so generates steam in the column which is at 110°F. (43.33°C.) without requiring intro ⁇ duction of additional heat to the stripping column.
  • the inven- tion provides an economical process and system for efficient recovery of working fluid from geothermal brine or other hot water containing sources employed in direct contact heat exchange for recovery of energy, comprising a unique combination of steps or operations, in which a portion of the working fluid dissolved and/or entrained in such brine or water is removed in successive increments, in such a manner that following the last step or stage of working fluid removal, the discharged brine or hot water is substantially free of working fluid, or the amount thereof remaining in the spent brine or water is so small as to be commercially non-recovera ⁇ ble.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)

Abstract

Pour la recuperation d'energie a partir de saumures geothermiques et d'autres sources contenant de l'eau ou de l'eau chaude, la saumure ou l'eau chaude sous pression est introduite dans le haut d'une colonne d'echange de chaleur (20) ou elle echange de la chaleur par contact direct avec un fluide de travail, tel que de l'isobutane. L'isobutane chaud ainsi obtenu est detendu dans une turbine (28) pour produire du travail et passe dans un condenseur (34). Le fluide de travail condense retourne vers l'echangeur de chaleur (20) et la saumure refroidie est retiree du fond de l'echangeur de chaleur (20). Il s'agit de recuperer le fluide de travail qui est dissout et/ou entraine dans la saumure geothermique epuisee ou dans l'eau retiree de l'echangeur de chaleur a contact direct (20). Ceci comprend les etapes de decantation la saumure dans un decanteur (52) pour recuperer une partie de l'isobutane, d'introduire la saumure restante dans un ballon de detente (68) pour obtenir une partie supplementaire d'isobutane et de rectifier la saumure epuisee a l'aide de vapeur dans une colonne de rectification. L'isobutane recupere dans chaque etape est dirige vers l'echangeur de chaleur a contact direct (20).
PCT/US1979/000052 1978-02-06 1979-02-02 Procede et installation pour la recuperation du fluide de travail d'un echangeur de chaleur a contact direct WO1979000589A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US875213 1978-02-06
US05/875,213 US4272960A (en) 1978-02-06 1978-02-06 Process and system for recovery of working fluid for direct contact heat exchange

Publications (1)

Publication Number Publication Date
WO1979000589A1 true WO1979000589A1 (fr) 1979-08-23

Family

ID=25365390

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US1979/000052 WO1979000589A1 (fr) 1978-02-06 1979-02-02 Procede et installation pour la recuperation du fluide de travail d'un echangeur de chaleur a contact direct

Country Status (5)

Country Link
US (1) US4272960A (fr)
JP (1) JPS55500072A (fr)
IT (1) IT1110262B (fr)
NZ (1) NZ189580A (fr)
WO (1) WO1979000589A1 (fr)

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US4521689A (en) * 1983-02-24 1985-06-04 General Electric Company Modular radiation-detecting array
US5458798A (en) * 1993-02-05 1995-10-17 E. I. Du Pont De Nemours And Company Azeotropic and azeotrope-like compositions of a hydrofluorocarbon and a hydrocarbon
US6119458A (en) * 1998-12-29 2000-09-19 Harris; James Jeffrey Immiscible, direct contact, floating bed enhanced, liquid/liquid heat transfer process
US6606868B1 (en) 1999-10-04 2003-08-19 Refrigerant Products, Ltd. R 22 replacement refrigerant
US6629419B1 (en) 1999-10-04 2003-10-07 Refringerant Products Ltd. CFC 12 replacement refrigerant
US6604368B1 (en) 1999-10-04 2003-08-12 Refrigerant Products, Ltd. R 12 replacement refrigerant
GB0206413D0 (en) * 2002-03-19 2002-05-01 Refrigerant Products Ltd Refrigerant for centrifugal compressors
GB0404343D0 (en) * 2004-02-27 2004-03-31 Rpl Holdings Ltd Refrigerant composition
CA2644560C (fr) * 2006-03-03 2014-10-14 Rpl Holdings Limited Composition refrigerante
PT2013309E (pt) * 2006-03-03 2014-12-03 Rpl Holdings Ltd Composição refrigerante
GB0908063D0 (en) * 2009-05-11 2009-06-24 Atalla Naji A Apparatus for thermal efficient power generation and method therefor
GB0922288D0 (en) 2009-12-21 2010-02-03 Rpl Holdings Ltd Non ozone depleting and low global warming potential refrigerants for refrigeration
US9599404B2 (en) 2013-08-27 2017-03-21 Black Night Enterprises, Inc. Fluid direct contact heat exchange apparatus and method
DE102014202846A1 (de) * 2014-02-17 2015-08-20 Siemens Aktiengesellschaft Verfahren und Vorrichtung zum Entladen eines thermischen Schichtspeichers
DE102014202849A1 (de) * 2014-02-17 2015-08-20 Siemens Aktiengesellschaft Verfahren und Vorrichtung zum Beladen eines thermischen Schichtspeichers
US10330364B2 (en) 2014-06-26 2019-06-25 Hudson Technologies, Inc. System and method for retrofitting a refrigeration system from HCFC to HFC refrigerant
GB201505230D0 (en) 2015-03-27 2015-05-13 Rpl Holdings Ltd Non ozone depleting and low global warming refrigerant blends
AU2018373915B2 (en) 2017-11-27 2024-02-22 Rpl Holdings Limited Low GWP refrigerant blends
CN110064220B (zh) * 2019-05-27 2024-06-14 昆明理工大学 一种料液以薄层和液滴流运动的微波强化连续闪蒸系统
MX2023004622A (es) 2020-10-22 2023-05-12 Rpl Holdings Ltd Refrigerantes de bomba termica.

Citations (5)

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Publication number Priority date Publication date Assignee Title
US2113130A (en) * 1935-08-17 1938-04-05 Socony Vacuum Oil Co Inc Method of distillation
US2520006A (en) * 1944-10-11 1950-08-22 Standard Oil Dev Co Vapor liquid solvent extraction process
US3414482A (en) * 1966-08-01 1968-12-03 Phillips Petroleum Co Preventing fractionator reboiler fouling
US3988895A (en) * 1974-01-11 1976-11-02 Itzhak Sheinbaum Power generation from hot brines
US4089175A (en) * 1975-06-23 1978-05-16 Occidental Petroleum Corporation Process and system for recovery of energy from geothermal brines and other water containing sources by direct contact with a working fluid below the critical pressure

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2342263A1 (fr) * 1976-02-27 1977-09-23 Raffinage Cie Francaise Procede d'obtention d'isobutylene d'une purete superieure a 99,5 % en poids

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2113130A (en) * 1935-08-17 1938-04-05 Socony Vacuum Oil Co Inc Method of distillation
US2520006A (en) * 1944-10-11 1950-08-22 Standard Oil Dev Co Vapor liquid solvent extraction process
US3414482A (en) * 1966-08-01 1968-12-03 Phillips Petroleum Co Preventing fractionator reboiler fouling
US3988895A (en) * 1974-01-11 1976-11-02 Itzhak Sheinbaum Power generation from hot brines
US4089175A (en) * 1975-06-23 1978-05-16 Occidental Petroleum Corporation Process and system for recovery of energy from geothermal brines and other water containing sources by direct contact with a working fluid below the critical pressure

Also Published As

Publication number Publication date
IT7919923A0 (it) 1979-02-06
NZ189580A (en) 1983-02-15
IT1110262B (it) 1985-12-23
JPS55500072A (fr) 1980-02-07
US4272960A (en) 1981-06-16

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